CN109054915A - A kind of throttling pre-dehydration, the regenerated Gas Dehydration System of entrainer and method - Google Patents

A kind of throttling pre-dehydration, the regenerated Gas Dehydration System of entrainer and method Download PDF

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Publication number
CN109054915A
CN109054915A CN201810748102.XA CN201810748102A CN109054915A CN 109054915 A CN109054915 A CN 109054915A CN 201810748102 A CN201810748102 A CN 201810748102A CN 109054915 A CN109054915 A CN 109054915A
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gas
entrainer
dehydration
absorption tower
liquid
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CN109054915B (en
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周树青
仝淑月
曹学文
边江
高继峰
李光
周圣钊
杜翰
宋晓丹
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Sinopec Oilfield Service Corp
Sinopec Zhongyuan Petroleum Engineering Design Co Ltd
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Sinopec Oilfield Service Corp
Sinopec Zhongyuan Petroleum Engineering Design Co Ltd
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/106—Removal of contaminants of water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1493—Selection of liquid materials for use as absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/26—Drying gases or vapours
    • B01D53/263—Drying gases or vapours by absorption
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/202—Alcohols or their derivatives
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons
    • B01D2256/245—Methane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/80—Water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/541—Absorption of impurities during preparation or upgrading of a fuel

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Organic Chemistry (AREA)
  • Gas Separation By Absorption (AREA)
  • Drying Of Gases (AREA)

Abstract

The invention belongs to natural gas processing technical fields, and in particular to a kind of throttling pre-dehydration, the regenerated Gas Dehydration System of entrainer and method.Laval jet pipe and gas-liquid separator are set before absorption tower, carry out the pre-dehydration of natural gas.Entrainer squeezes into reboiler from azeotropic regenerative circuit, mouth is provided at the top of regenerator, it will be drawn containing the high-temperature gas of entrainer and water, after heat exchanger and lean solution heat exchange, using three phase separator, the separation of entrainer and water, gas is realized, the entrainer after separation is after entrainer drier is dry, it is delivered to reboiler through circulating pump again, realizes the recycling of entrainer.Gas gas current divider is set after absorption tower, the dry gas after absorption tower is dry is most of outer defeated, and another small portion of gas reaches stripping column bottom and makees stripping gas.The present invention solves the problems, such as existing TEG dehydration device, and existing low efficiency and energy consumption are high in the process of running, are not able to satisfy deep dehydration requirement.

Description

A kind of throttling pre-dehydration, the regenerated Gas Dehydration System of entrainer and method
Technical field
The invention belongs to natural gas processing technical fields, and in particular to a kind of throttling pre-dehydration, entrainer are regenerated natural Qi exhaustion water system and method.
Background technique
The natural gas of well head outflow is nearly all saturated by gas phase water, or even can carry a certain amount of liquid water.Natural gas The presence of middle moisture often will cause serious consequence: containing CO2And H2The natural gas of S forms acid in the presence of water And corrode pipeline and equipment；It forms gas hydrates under certain condition and blocks valve, pipeline and equipment；It is defeated to reduce pipeline Ability is sent, unnecessary power consumption is caused.Moisture is very unfavorable thing in the presence of natural gas, and therefore, it is necessary to dehydrations It is required that more stringent.The main method of the dewatering of natural gas has low temperature processing, solvent absorption, solid absorption method, answers Use membrane separation process.
Low temperature processing dehydration: being the temperature difference by means of natural gas and condensation vapor for liquid, in certain pressure The lower temperature for reducing saturated gas, makes steam therein and heavy hydrocarbon is condensed into liquid, then by means of the relatively close of liquid hydrocarbon and water Degree difference and mutually insoluble feature carry out Gravity Separation, deviate from water.Low temperature processing is cooled down by throttling expansion or outside Refrigeration, so that elutriation in natural gas be made to go out.Gas water dew point depends primarily on the gas temperature after throttling after dehydration, if needing to increase When pressing or adding external refrigeration, the investment of device and operating cost are higher.This method has been generally used for pressure energy (pressure drop) can The high pressure natural gas dehydration utilized can control gas water dew point and hydrocarbon dew point simultaneously.Existing technical problem underlying is as follows: 1) It needs injecting inhibitor (common methanol or ethylene glycol) to prevent gas hydrates, to build inhibitor injection and regenerative system；2) It is difficult to separate there are alcohol hydrocarbon, the problems such as inhibitor is lossy；3) system equipment is more, process flow is complicated.
Solid absorption dehydration: being to have stronger suction-operated and selection to steam in natural gas with certain solid matters Property makes in natural gas Vapor adsorption on the surface of solids, to other components do not adsorb or adsorb it is less, to realize natural gas Dehydration.The active aluminium oxide of industrial common adsorption dehydrating agent, silica gel, molecular sieve, wherein molecular sieve dehydration application is the widest It is general.Water content can be down to 1ppm after gas dehydration, and water dew point drop is mainly used for CNG gas station, natural airsetting up to 120 DEG C Liquid recyclable device, natural gas liquefaction device even depth are dehydrated place.Absorption method dehydration is: 1) for large size Device, equipment investment is big, and operating cost is high；2) adsorbent service life is short, must generally be replaced, be increased into using 3 years This；4) energy consumption is high, regenerates large-minded, and when low processing capacity becomes apparent from.
UF membrane dehydration: being the preferential differential permeability using membrane material to steam in natural gas, when natural gas flow is through film When surface, steam preferentially penetrates film and is removed and deviates from natural gas steam.Compared with traditional dewatering, embrane method is de- The advantages that water has simple process, and operation is easy, is not required to that solvent additionally is added, without secondary pollution, and the pressure loss is smaller, but mesh Before, the dehydration of natural gas UF membrane has industrial application in states such as the U.S., Japan, Canada.1998, the big fluidization of the Chinese Academy of Sciences Object institute and Changqing Petroleum Exploration Bureau of China National Petroleum Corporation (CNPC) have developed Natural Gas Dehydration Based on Membrane Tech-nology industrial experiment dress cooperatively It sets, and has carried out operation in more than 1700 hours.The device day output (3~15) × 104Nm3, the dew-point temperature control of product gas - 28~-8 DEG C (its discharge pressure is less than 4.6MPa), methane recovery >=98%, film properties are stablized.The master of UF membrane dehydration Wanting technical problem is: 1) the gas separation membrane country is in the research and development stage, and inlet device price is higher；2) membrane material reliability It is poor, bearing capacity is limited；3) plant investment is dehydrated high than triethylene glycol.
Solvent absorption dehydration: being to have good absorption and dissolubility to steam in natural gas using certain liquid substances Can, steam in natural gas is deviate from.Dewatered solution vapor pressure is very low and renewable and is recycled.Solvent absorption dehydration Method is using a kind of more universal method in current gas dehydration, wherein being applied in gas dehydration with triethylene glycol dehydration Extensively, gas water depoint depression is up to 40 DEG C, can meet natural gas tube is defeated, in gas reducing liquid recycling shallow cold technique to water dew point Requirement.TEG dehydration system includes separator, absorption tower and triethylene glycol regenerative system.Triethylene glycol is dehydrated existing main skill Art problem is as follows: 1) systematic comparison is complicated, the energy consumption of triethylene glycol. solution regenerative process is bigger；2) triethylene glycol. solution can lose and It is contaminated, it requires supplementation with and purifies；3) triethylene glycol is contacted with air can occur oxidation reaction, generate mordant organic acid. Triethylene glycol has many advantages, such as that water absorbing force is strong, solubility is low, boiling point is high, easy regeneration, invests small, applies in current dewatering process The most extensively, but at one atm, when the temperature of reboiler reaches 200 DEG C, obtained by conventional triethylene glycol dewatering process flow Triethylene glycol lean solution concentration it is low, for be dehydrated the higher situation of depth requirements so that dewatering process flow be unable to reach dehydration require.
Summary of the invention
It is regenerated it is an object of the invention to provide a kind of throttling pre-dehydration, azeotropic aiming at the problems existing in the prior art New and effective dewatering system and method, the system and method solve existing TEG dehydration system and exist in the process of running Low efficiency and the high problem of energy consumption, especially when the temperature of reboiler reaches 200 DEG C, obtained by conventional triethylene glycol dewatering process flow The problem of triethylene glycol lean solution concentration arrived is low, is unable to reach deep dehydration requirement.
The technical scheme is that
A kind of throttling pre-dehydration, the regenerated Gas Dehydration System of entrainer, including sequentially connected gas-liquid separator and Absorption tower, the gas isolated in gas-liquid separator enter absorption tower, gas in the absorption tower after heating by heater Entering gas gas current divider by top exit, liquid enters flash tank by pipeline by bottom leakage fluid dram in the absorption tower, Flash tank bottom leakage fluid dram is connect with regenerator, and regenerator connects reboiler, and reboiler is connect with stripping columns, and described is wet natural Gas enters in gas-liquid separator through Laval jet pipe；The leakage fluid dram of the stripping columns is connect by pipeline with absorption tower；Described Regenerator top exit is connect after heat exchanger exchanges heat with three phase separator by pipeline；Gas in three phase separator goes out through gas Mouth discharge, liquid are exported through liquid and are discharged, and the entrainer isolated is recycled after entrainer drier is dry into reboiler It uses；The portion gas of the gas gas current divider enters stripping columns after heat exchanger heats.
Specifically, heat exchanger one is arranged between the absorption tower top exit and gas gas current divider.
Specifically, being provided with heat exchanger three and circulating pump on pipeline between the leakage fluid dram and absorption tower of the stripping columns One, and pass through heat exchanger one.
It is dodged specifically, entering after liquid is heated by pipeline through heat exchanger two by bottom leakage fluid dram in the absorption tower Steaming pot, and throttle valve is provided on pipeline.
The method for carrying out gas dehydration using system as described above, includes the following steps:
One, the wet gas come from gas gathering station, creates low temperature environment for fluid adiabatic expansion by Laval jet pipe, makes Heavy hydrocarbon and hydrogenesis in natural gas are drop, realize preliminary gas-liquid separation by gas-liquid separator；
Two, the heated device heating of natural gas after pre-dehydration, into absorption tower lower part, since gas phase is molten for glycol Liquid density is small, floats naturally, comes into full contact with the triethylene glycol lean solution in absorption tower from top to down, remove a part of water, become dry Gas reaches defeated outside natural gas and requires then by the outlet mouth of gas gas current divider through defeated outside the progress of dry gas multi-purpose station pipeline；
Three, triethylene glycol rich solution from absorbing tower bottom flow out, after reducing pressure by regulating flow, with regenerator top outflow gas into Row heat exchange, enters flash tank after promoting temperature, and the light hydrocarbon components such as most of methane, warp in triethylene glycol rich solution are removed in flash tank Cross it is stable after rich solution reducing pressure by regulating flow again, and enter regenerator after the heat exchange of stripping columns high temperature lean solution, through mentioning in regenerator The reboiling that section, rectifying section, overhead reflux pass through reboiler later is evaporated, the triethylene glycol. solution of higher concentration is obtained, using stripping Column further purifies, and reaches to 99.3% concentration, meets triethylene glycol dehydration concentration, is pumped in indentation absorption tower using circulation Circulation carries out gas dehydration；
Four, contain water and entrainer in the high-temperature gas flowed out at the top of regenerator, in order to realize the recycling of entrainer, Nonvoluntary discharge emptying, the gas with lean solution after exchanging heat, and using three phase separator, realizes entrainer and water, gas Separation, the entrainer after separation are delivered to reboiler after entrainer drier is dry, then through circulating pump, realize following for entrainer Ring uses；
Five, another part gas distributed by gas gas current divider reaches stripping columns, from air lift after heater heats The injection of column bottom lean solution part, as the triethylene glycol. solution in stripping gas and air lift column with heat, and the two flow direction is on the contrary, fill The steam partial pressure of tap touching, solution surface reduces, and is improved glycol liquid quality fraction to 99.8% or more.
The beneficial effects of the present invention are: the triethylene glycol lean solution concentration that 1. dewatering systems provided by the invention obtain is higher, by In regeneration, dewatering process entrainer is not soluble in water and triethylene glycol, therefore the triethylene glycol lean solution loss amount in dewatering process is less, Regenerate the triethylene glycol lean solution loss amount in dewatering process is about traditional TEG Dehydration Processing 10%；2. since the present invention provides System and method in triethylene glycol loss amount it is few, the triethylene glycol lean solution concentration recycled is high, passes through azeotropic regeneration dehydration system 38 DEG C lower than traditional TEG Dehydration Processing of dry gas water dew point or so after system dehydration；3. in system provided by the invention, When the temperature of reboiler reaches 200 DEG C, the mass fraction of glycol solution is improved to 99.8% or more, can achieve depth Dehydration requires；4. the present invention provides dewatering system, the dehydration effect of whole system is effectively raised after Laval jet pipe pre-dehydration Rate, while plant energy consumption is reduced, help to realize saving and environmental protection.
Detailed description of the invention
Fig. 1 is system structure diagram of the invention；
Fig. 2 is azeotropic regenerative circuit structural schematic diagram.
1 wet gas, 2Laval jet pipe, 3 gas-liquid separators, 4 throttle valves, 5 drainage pipelines, 6 heaters, 7 absorption towers, 8- 1 heat exchanger one, 8-2 heat exchanger two, 8-3 heat exchanger three, 9 gas gas current dividers, 10 dry gas multi-purpose station pipelines, 11 flash tanks, 12 tops Gas outlet, the outlet of 13 regenerators, 14 reboilers, 15 stripping columns, 16 gas, 17-1 circulating pump one, 17-2 circulating pump two, 18 entrainers Drier, 19 three phase separators, the outlet of 20 liquid.
Specific embodiment
As shown in Figure 1 it is a kind of throttling pre-dehydration, the regenerated Gas Dehydration System of entrainer structural schematic diagram, including according to The gas-liquid separator 3 of secondary connection and absorption tower 7, the gas isolated in gas-liquid separator 3 enters after being heated by heater 6 to be inhaled Receive tower 7, gas enters gas gas current divider 9 by top exit in the absorption tower 7,7 top exit of absorption tower and One 8-1 of heat exchanger is set between gas gas current divider 9；Liquid passes through pipeline through exchanging heat by bottom leakage fluid dram in the absorption tower 7 Enter flash tank 11 after two 8-2 of device heating, and is provided with throttle valve 4 on pipeline, 11 bottom leakage fluid dram of flash tank and regenerator 13 connections, regenerator 13 connect reboiler 14, and reboiler 14 is connect with stripping columns 15, and the wet gas 1 is through Laval jet pipe 2 enter in gas-liquid separator 3；The leakage fluid dram of the stripping columns 15 is connect by pipeline with absorption tower 7, the stripping columns 15 Leakage fluid dram and absorption tower 7 between pipeline on be provided with one 17-1 of three 8-3 of heat exchanger and circulating pump, and pass through one 8- of heat exchanger 1；13 top exit of regenerator is connect after heat exchanger 8-2 heat exchange with three phase separator 19 by pipeline；Three phase separation Gas in device 19 is through 16 discharge of gas outlet, and liquid is through 20 discharge of liquid outlet, and the entrainer isolated is through entrainer drier 18 Enter reboiler 14 after drying to be recycled；The portion gas of the gas gas current divider 9 enters after the heating of heat exchanger 6 Stripping columns 15.
The method for carrying out gas dehydration using system as described above, includes the following steps:
One, the wet gas 1 come from gas gathering station, creates low temperature environment for fluid adiabatic expansion by Laval jet pipe 2, Make the heavy hydrocarbon and hydrogenesis drop in natural gas, realizes preliminary gas-liquid separation by gas-liquid separator 3；
Two, the heated device 6 of natural gas after pre-dehydration heats, into 7 lower part of absorption tower, since gas phase is for glycol Solution density is small, floats naturally, comes into full contact with the triethylene glycol lean solution in absorption tower 7 from top to down, remove a part of water, become Dry gas reaches defeated outside natural gas and requires and then carried out by the outlet mouth of gas gas current divider 9 through dry gas multi-purpose station pipeline 10 outer defeated；
Three, triethylene glycol rich solution is flowed out from 7 tower bottom of absorption tower, the gas after reducing pressure by regulating flow, with the outflow of 13 top of regenerator Body exchanges heat, and enters flash tank 11 after promoting temperature, and it is light that most of methane etc. in triethylene glycol rich solution is removed in flash tank 11 The hydrocarbon component, rich solution after stabilization enter regenerator 13 after reducing pressure by regulating flow, with the heat exchange of 15 high temperature lean solution of stripping columns again, The reboiling for passing through reboiler 14 in regenerator 13 after stripping section, rectifying section, overhead reflux, obtains the triethylene glycol of higher concentration Solution is further purified using stripping columns 15, is reached to 99.3% concentration, meets triethylene glycol dehydration concentration, using following Ring is pumped circulation in 17-1 indentation absorption tower 7, carries out gas dehydration；
Four, entrainer squeezes into reboiler 13 from azeotropic regenerative circuit, under the conditions of identical reboiler temperature, can substantially reduce The water volume fraction of poor glycol in reboiler 13.Contain water and entrainer in the high-temperature gas flowed out at the top of regenerator 13, in order to Realize the recycling of entrainer, nonvoluntary discharge emptying, the gas with lean solution after exchanging heat, using three phase separator 19, realize the separation of entrainer and water, gas, entrainer after separation is after entrainer drier 18 is dry, then through circulating pump 17-2 is delivered to reboiler 14, realizes the recycling of entrainer, by adding azeotropic regenerative circuit, can substantially reduce reboiling The boiling point of water in device makes the water volume fraction in poor glycol that can be reduced to about 10 × 10 from 0.1%-6；
Five, another part gas distributed by gas gas current divider 9 reaches stripping columns 15 after the heating of heater 6, from The injection of 15 bottom lean solution part of air lift column, it is same hot as the triethylene glycol. solution in stripping gas and air lift column 15, and the two flowing side To on the contrary, come into full contact with, the steam partial pressure of solution surface is reduced, make glycol liquid quality fraction be improved to 99.8% with On.
The present invention be in order to solve existing TEG dehydration device in the process of running existing low efficiency and energy consumption it is high, Not the problem of not being able to satisfy deep dehydration requirement.Laval jet pipe 2 and gas-liquid separator 3, gas-liquid point are set before the absorption tower 7 It is discharged from bottom discharge outlet 5 from the water that device 3 is isolated, carries out the pre-dehydration of natural gas.The entrainer from azeotropic again Reboiler 14 is squeezed into raw circuit, under the conditions of identical 14 temperature of reboiler, reduces the boiling point of water to substantially reduce reboiler The water volume fraction of poor glycol in 14.Outlet is set at the top of regenerator 7, will draw, pass through containing the high-temperature gas of entrainer and water After heat exchanger 6 and lean solution heat exchange, using three phase separator 19, the separation of entrainer and water, gas, the azeotropic after separation are realized Agent is delivered to reboiler 14 after entrainer drier 18 is dry, then through circulating pump 17-2, realizes the recycling of entrainer.Institute Gas gas current divider 9 is set after the absorption tower 7 stated, most of outer defeated, another small portion of gas of the dry gas after absorption tower 7 is dry After the decompression of throttle valve 4, heater 6 heat, reaches 15 bottom of stripping columns and make stripping gas, gas flow can be in gas gas current divider 9 Middle adjusting, to meet the needs of stripping columns 15.
Finally it should be noted that: the above embodiments are merely illustrative of the technical scheme of the present invention and are not intended to be limiting thereof；To the greatest extent The present invention is described in detail with reference to preferred embodiments for pipe, it should be understood by those ordinary skilled in the art that: still It can modify to a specific embodiment of the invention or some technical features can be equivalently replaced；Without departing from this hair The spirit of bright technical solution should all cover within the scope of the technical scheme claimed by the invention.

Claims (5)

1. a kind of throttling pre-dehydration, the regenerated Gas Dehydration System of entrainer, including sequentially connected gas-liquid separator (3) and Absorption tower (7), the gas isolated in gas-liquid separator (3) enter absorption tower (7) after heating by heater 6, the suction Gas enters gas gas current divider (9) by top exit in receipts tower 7, and liquid is passed through by bottom leakage fluid dram in the absorption tower 7 Pipeline enters flash tank (11), and flash tank (11) bottom leakage fluid dram is connect with regenerator (13), and regenerator (13) connects reboiler (14), reboiler (14) is connect with stripping columns (15), which is characterized in that the wet gas 1 enters gas through Laval jet pipe 2 In liquid/gas separator 3；The leakage fluid dram of the stripping columns (15) is connect by pipeline with absorption tower (7)；The regenerator (13) Top exit is connect after heat exchanger 8-2 heat exchange with three phase separator (19) by pipeline；Gas in three phase separator (19) Through 16 discharge of gas outlet, through 20 discharge of liquid outlet, the entrainer isolated enters liquid after entrainer drier (18) are dry Reboiler (14) is recycled；The portion gas of the gas gas current divider (9) enters stripping columns after the heating of heat exchanger 6 (15)。
2. throttle pre-dehydration, the regenerated Gas Dehydration System of entrainer according to claim 1, which is characterized in that described 7 top exit of absorption tower and gas gas current divider (9) between be arranged one 8-1 of heat exchanger.
3. throttle pre-dehydration, the regenerated Gas Dehydration System of entrainer according to claim 2, which is characterized in that described Stripping columns (15) leakage fluid dram and absorption tower (7) between pipeline on be provided with one 17-1 of three 8-3 of heat exchanger and circulating pump, and By one 8-1 of heat exchanger.
4. throttle pre-dehydration, the regenerated Gas Dehydration System of entrainer according to claim 1, which is characterized in that described Absorption tower 7 in liquid by bottom leakage fluid dram flash tank (11) are entered after two 8-2 of heat exchanger heating by pipeline, and pipeline On be provided with throttle valve 4.
5. the as above method that system described in any claim carries out gas dehydration, which comprises the steps of:
One, the wet gas 1 come from gas gathering station, creates low temperature environment for fluid adiabatic expansion by Laval jet pipe 2, makes day Heavy hydrocarbon and hydrogenesis in right gas are drop, realize preliminary gas-liquid separation by gas-liquid separator 3；
Two, the heated device 6 of natural gas after pre-dehydration heats, into 7 lower part of absorption tower, since gas phase is for glycol solution Density is small, floats naturally, comes into full contact with the triethylene glycol lean solution in absorption tower 7 from top to down, remove a part of water, become dry Gas reaches defeated outside natural gas and requires and then carried out by the outlet mouth of gas gas current divider (9) through dry gas multi-purpose station pipeline 10 outer defeated；
Three, triethylene glycol rich solution from 7 tower bottom of absorption tower flow out, after reducing pressure by regulating flow, with 13 top of regenerator outflow gas into Row heat exchange, enters flash tank 11 after promoting temperature, and the lighter hydrocarbons group such as most of methane in triethylene glycol rich solution is removed in flash tank 11 Point, reducing pressure by regulating flow is regenerating the rich solution after stabilization into regenerator 13 after exchanging heat with 15 high temperature lean solution of stripping columns again Pass through the reboiling of reboiler 14 in tower 13 after stripping section, rectifying section, overhead reflux, the triethylene glycol for obtaining higher concentration is molten Liquid is further purified using stripping columns 15, is reached to 99.3% concentration, meets triethylene glycol dehydration concentration, using circulation It is pumped circulation in 17-1 indentation absorption tower 7, carries out gas dehydration；
Four, contain water and entrainer in the high-temperature gas flowed out at the top of regenerator 13, in order to realize the recycling of entrainer, no Arbitrarily discharge emptying, the gas with lean solution after exchanging heat, and using three phase separator 19, realizes entrainer and water, gas Separation, the entrainer after separation are delivered to reboiler 14 after entrainer drier 18 is dry, then through circulating pump 17-2, realize altogether Boil the recycling of agent；
Five, another part gas distributed by gas gas current divider 9 reaches stripping columns 15, from air lift after the heating of heater 6 The injection of 15 bottom lean solution part of column, it is same hot as the triethylene glycol. solution in stripping gas and air lift column 15, and the two flow direction phase Instead, it comes into full contact with, the steam partial pressure of solution surface reduces, and is improved glycol liquid quality fraction to 99.8% or more.
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CN111302897A (en) * 2020-03-23 2020-06-19 西南石油大学 Energy-saving and simple methanol regeneration and recovery process device and method
CN111454758A (en) * 2020-04-10 2020-07-28 北京石油化工学院 Efficient compact natural gas glycol dehydration system and method
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